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US7964677B2 - Method of changing between incompatible polymerization catalysts in a gas-phase fluidized-bed reactor - Google Patents

Method of changing between incompatible polymerization catalysts in a gas-phase fluidized-bed reactor Download PDF

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US7964677B2
US7964677B2 US12/085,079 US8507906A US7964677B2 US 7964677 B2 US7964677 B2 US 7964677B2 US 8507906 A US8507906 A US 8507906A US 7964677 B2 US7964677 B2 US 7964677B2
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polymerization
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US20090062486A1 (en
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Shahram Mihan
Rainer Karer
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Basell Polyolefine GmbH
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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F210/16—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S526/00—Synthetic resins or natural rubbers -- part of the class 520 series
    • Y10S526/901—Monomer polymerized in vapor state in presence of transition metal containing catalyst

Definitions

  • the invention relates to a method of changing from a first catalyst to a second catalyst which is incompatible with the first catalyst.
  • Gas-phase polymerization processes are economical processes for the polymerization of C 2 -C 8 - ⁇ -olefins. Such gas-phase polymerization processes can, in particular, be carried out as gas-phase fluidized-bed processes in which the polymer particles are kept suspended by means of an appropriate gas stream. Processes of this type are described, for example, in EP-A-0 475 603, EP-A-0 089 691 and EP-A-0 571 826, whose contents are hereby fully incorporated by reference.
  • WO 00/58377 discloses a discontinuous method of changing from a first catalyst to a second incompatible catalyst, in which the polymerization using the first catalyst is stopped, the polymer is removed from the reactor, the reactor is flushed with nitrogen, a new particle bed is introduced into the reactor and the polymerization is continued using the second catalyst.
  • the opening of the reactor leads to deposits on the walls which have an adverse effect on the renewed start-up of the reactor.
  • EP-A-751965 describes a continuous method of changing catalyst from a first catalyst to a second catalyst incompatible with the first, in which the introduction of the first catalyst is interrupted, an reversible and optionally an irreversible catalyst poison is added in excess, the reactor is flushed and the second catalyst is introduced into the reactor.
  • contamination of the reactor with water and air can be avoided in this way, a mixed polymer which is only in rare cases within the specification of the old or new product leaves the reactor for a prolonged transition time (a multiple of the mean residence time).
  • the first catalyst has to be titrated with an equimolar amount of catalyst poison, with too little catalyst poison leading to unsatisfactory deactivation of the first catalyst and too large an amount also deactivating the new catalyst.
  • WO 2004/060931 discloses the use of a relatively nonvolatile deactivating agent having a vapor pressure under reaction conditions of less than 133 Pa in a method of changing from a Ziegler-Natta catalyst to an MAO-based single-site catalyst which is incompatible with the first catalyst.
  • WO 2004/060930 also provides for the use of a deactivating agent selected from among oxygen, air, CO, CO 2 , H 2 O, oleic acid and NH 3 to stop the reaction with the metallocene catalyst in a method of changing from a metallocene catalyst to a catalyst in compatible therewith.
  • the discontinuous methods have the disadvantage that either the start-up of the reactor leads to stable conditions in the reactor only after a number of starts or is very time-consuming.
  • the methods which are less time-consuming and lead to satisfactory results are, on the other hand, tailored very specifically to a particular catalyst change, so that various change-over methods using different equipment and reagents have to be kept on hand.
  • This object is achieved according to the invention by a method of changing from a polymerization using a first catalyst to a polymerization using a second catalyst which is incompatible with the first catalyst in a gas-phase reactor, which comprises the steps
  • the present invention makes it possible to carry out a catalyst change when using different incompatible catalysts reliably and simply.
  • Incompatible catalysts are, for the purposes of the present invention, ones which fulfill at least one of the following conditions:
  • the polymerization reaction using the first catalyst is stopped in step a).
  • This can be achieved in various ways, for example by simply stopping the introduction of catalyst, by introducing a deactivating agent or by reducing the temperature, the pressure or the monomer concentration in the reactor. A combination of the abovementioned ways of stopping the reaction is also possible.
  • the reaction is preferably stopped by means of CO 2 .
  • the reaction is preferably stopped using oxygen or lean air, i.e. air which has a reduced proportion of oxygen.
  • the reactor is subsequently flushed in step b) with a deactivating agent comprising a volatile constituent and a nonvolatile constituent under polymerization conditions.
  • a deactivating agent comprising a volatile constituent and a nonvolatile constituent under polymerization conditions. This can be effected while retaining the particle bed present in the reactor or after emptying and filling with a new particle bed, with the latter being preferred.
  • a preferred embodiment of the present invention provides for the reactor to be emptied completely in a step a′) and filled with a new particle bed (flushing bed) for carrying out step b).
  • a volatile constituent of the deactivating agent is a substance or a mixture which has a vapor pressure of above 1000 Pa under the conditions in the recycle gas system. It is important that the vapor pressure is sufficiently high to ensure complete deactivation of the catalyst present in the recycle gas system. Preference is given to a vapor pressure of above 1500 Pa, preferably above 2000 Pa, at 20° C. Preference is also given to the volatile component having a boiling point below the temperature in the gas-phase fluidized-bed reactor under polymerization conditions, so that it vaporizes completely in the reactor.
  • a nonvolatile constituent of the deactivating agent is a substance or a mixture which does not go into the gas phase, or at most goes into the gas phase in small amounts, under polymerization conditions and therefore acts essentially only in the reactor itself. It preferably has a vapor pressure of less than 1000 Pa, particularly preferably less than 100 Pa, at 20° C.
  • the nonvolatile constituent preferably not only completely deactivates the catalyst in the reactor but also leaves a thin film on the reactor surface and thus aids renewed start-up.
  • the volatile constituent (V) and the nonvolatile constituent (N) are present in the deactivating agent in a weight ratio V/N of from 0.1 to 1000. Preference is given to using a weight ratio V/N of from 0.5 to 400, more preferably from 1 to 300. Particular preference is given to using the volatile constituent in a weight excess, preferably in a ratio of from 5 to 200, more preferably from 10 to 200, particularly preferably from 20 to 100.
  • further substances having a deactivating action can also be used in the reactor.
  • further auxiliaries such as antistatics, scavengers, etc., is possible.
  • the deactivating agent can comprise inert solvents, for example saturated hydrocarbons such as hexane.
  • the amount of deactivating agent used is dependent on the size and geometry of the reactor, so that is has to be adapted to the circumstances. It is possible, for example, to start with a small amount and increase it until complete deactivation has taken place.
  • the deactivating agent can be used in an amount of from 20 to 2000 g/h. Preference is given to amounts of from 100 to 1000 g/h, particularly preferably from 200 to 500 g/h.
  • both the volatile constituents (V) and the nonvolatile constituents (N) of the deactivating agent comprise substances or mixtures which are able to react with at least one of the catalyst constituents and thus make the catalyst inactive. Preference is given to constituents (V) or (N) which irreversibly deactivate the catalyst, i.e. no reactivation of the catalyst can be observed even when the deactivating agent is removed.
  • Suitable volatile constituents (V) are, for example, low molecular weight alcohols and their ethers, low molecular weight esters and amines which have a sufficient vapor pressure for them to be able to be present in gaseous form in a sufficient amount under the usual polymerization conditions and in particular also under the conditions in the recycle gas system.
  • nonvolatile constituents (N) are nonvolatile nitrogen-comprising compounds such as amines or amides or their salts, in particular oligomeric or polymeric amines and amides.
  • nonvolatile nitrogen-comprising compounds such as amines or amides or their salts, in particular oligomeric or polymeric amines and amides.
  • examples which may be mentioned are polyethoxyalkylamines and polyethoxyalkylamides of the general formulae R 1 N[(R 2 O) m R][(R 3 O) n H] and R 1 CON[(R 2 O) m R][(R 3 O) n H], where R 1 to R 3 are alkyl radicals.
  • R 1 preferably ones having at least 8 carbon atoms, more preferably at least 12 carbon atoms, and n, m are equal to or greater than 1, as described in DE-A 31 088 43.
  • These are also constituents of commercial antistatics (e.g. Atmer® 163; from Uniqema). It is also possible to use salt mixtures of calcium salts of Medialanic acid and chromium salts of N-stearylanthranilic acid, as in DE-A 3543360, whose contents are hereby fully incorporated by reference, or mixtures of a metal salt of Medialanic acid, a metal salt of anthranilic acid and a polyamine as described in EP-A 636 636.
  • nonvolatile constituents are polyamines or polyamine copolymers or mixtures of such compounds with further, in particular polymeric, compounds.
  • suitable nonvolatile polyamines are advantageously obtained from the reaction of aliphatic primary monoamines such as n-octylamine or n-dodecylamine or N-alkyl-substituted aliphatic diamines such as N-n-hexadecyl-1,3-propanediamine with epichlorohydrin.
  • aliphatic primary monoamines such as n-octylamine or n-dodecylamine or N-alkyl-substituted aliphatic diamines such as N-n-hexadecyl-1,3-propanediamine with epichlorohydrin.
  • These polyamino polyols have hydroxyl groups in addition to amino groups.
  • Polymers which are particularly suitable for use together with polyamines or polyamine copolymers are polysulfone copolymers.
  • the polysulfone copolymers are preferably largely unbranched and are made up of olefins and SO 2 units in a molar ratio of 1:1.
  • An example which may be mentioned is 1-decene polysulfone.
  • An overview of suitable polysulfone copolymers is also given in U.S. Pat. No. 3,917,466, whose contents are hereby fully incorporated by reference.
  • Particular preference is given to using a mixture comprising a C 1 -C 4 -alcohol as volatile component and a mixture of a polyethoxyalkylamine, a polyamino polyol and an alkylarylsulfonic acid as nonvolatile component.
  • Step b) takes place at temperatures of from 20 to 150° C., preferably at temperatures above 50° C., more preferably above 70° C. and particularly preferably above 90° C.
  • step b) preferably takes place at 10-1° C. below, particularly preferably 5-1° C. below, the sintering temperature of the polymer.
  • the second catalyst is introduced into the reactor, i.e. the metered addition of the second catalyst is commenced, in the subsequent step c).
  • the metering device for the first catalyst can be used after flushing or a separate metering device can be used.
  • Scavengers such as metal alkyls, in particular aluminum alkyls, which react with the moisture, oxygen and other catalyst poisons still present in the reactor are usually introduced before renewed start-up using the second catalyst.
  • a preferred embodiment of the present invention provides for the reactor to be emptied completely in a step b′) and filled with fresh polymer powder prior to step c).
  • Step d) the polymerization using the second catalyst is continued in step d).
  • Steps c) and d) are generally known to those skilled in the art.
  • the method of the invention is employed for changing the catalyst in a gas-phase reactor for the polymerization and copolymerization of ⁇ -olefins such as ethylene, propene, 1-butene, 1-pentene, 4-methyl-1-pentene, 1-hexene, 1-heptene and 1-octene.
  • ⁇ -olefins such as ethylene, propene, 1-butene, 1-pentene, 4-methyl-1-pentene, 1-hexene, 1-heptene and 1-octene.
  • Ethylene and propylene, in particular ethylene can be homopolymerized or copolymerized particularly well.
  • Possible comonomers are, in particular, ⁇ -olefins having from 3 to 8 carbon atoms, especially propene, 1-butene, 1-pentene, 4-methyl-1-pentene, 1-hexene, 1-heptene and 1-octene and also mixtures of these ⁇ -olefins.
  • the polymerization can be carried out according to various gas-phase processes, for example in a gas-phase fluidized bed or in a stirred gas phase.
  • gas-phase processes are known per se and are described, for example, in Ullmann's Encyclopedia of Industrial Chemistry, Vol. A 21, 4th Edition, 1992, p. 511ff, whose contents are hereby fully incorporated by reference. Preference is given to polymerization in a gas-phase fluldized-bed reactor.
  • the polymerization is carried out at temperatures of from 30 to 150° C., preferably from 80 to 120° C.
  • the pressure is in the range from 5 to 80 bar, preferably from 10 to 60 bar.
  • the polymerization is carried out at a temperature in a range delimited by an upper limit given by equation I
  • reaction temperature for the preparation of a polymer having the given density d must not exceed the value defined by equation I and must not be below the value defined by equation II but instead has to be between these limiting values.
  • EP-B-571 826 and EP-A-1040128 whose contents are hereby fully incorporated by reference, without this implying a restriction to the use of the corresponding catalysts.
  • the density d of the resulting (co)polymers and thus the reactor temperature to be advantageously selected is, in the method of the invention, determined essentially by the ratios of the starting materials used, in particular the ratio of ethylene to C 3 -C 6 - ⁇ -olefins.
  • the reactor can also be operated with proportions of condensed material being present, as described, for example, in EP-A-089 691 or EP-A-696 293.
  • the method of the invention is basically suitable for the change from any polymerization catalyst to any other incompatible catalyst. Both the first and second catalysts can therefore be selected freely according to the invention, as long as the two are incompatible.
  • the method is particularly suitable for the change from a single-site, Ziegler or hybrid catalyst to a chromium catalyst of from a Ziegler catalyst to a single-site or hybrid catalyst, without the process having to be altered, apart from slight adaptations.
  • Catalyst systems of the Ziegler-Natta type have been known for a long time. These systems are used, in particular, for the polymerization of C 2 -C 10 -alk-1-enes and comprise, inter alia, compounds of polyvalent titanium, aluminum halides and/or aluminum alkyls and also a suitable support material. Further details regarding Ziegler-Natta catalysts may be found, for example, in the patent applications EP-A-1184395, EP-A-1456249 or WO03099882.
  • Chromium catalysts of the Phillips type have likewise been known for a long time. They comprise an inert inorganic support, preferably silica gel, to which a chromium compound and, if appropriate, further transition metals such as titanium or zirconium are applied. The support is then usually calcined at temperatures of from 300 to 950° C.
  • single-site catalysts comprise, as a difference from Phillips and Ziegler/Natta catalysts, at least one defined organic transition metal compound and usually at least one further activating compound and, if appropriate, supports and further additives and auxiliaries.
  • Possible organic transition metal compounds for single-site catalysts are in principle all compounds of the transition metals of groups 3 to 12 of the Periodic Table or the lanthanides which comprise organic groups and, preferably after reaction with the activator and support, form active catalysts for olefin polymerization. They are usually compounds in which at least one monodentate or polydentate ligand is bound via a sigma or pi bond to the central atom. Possible ligands include both ones which comprise cyclopentadienyl radicals and ones which are free of cyclopentadienyl radicals. Many such compounds A) which are suitable for olefin polymerization are described in Chem. Rev. 2000, Vol. 100, No. 4. Furthermore, multinuclear cyclopentadienyl complexes are also suitable for olefin polymerization.
  • Suitable organic transition metal compounds are, in particular, ones having at least one cyclopentadienyl-type ligand, with those having two cyclopentadienyl-type ligands generally being referred to as metallocene complexes.
  • Particularly useful organic transition metal compounds A) having at least one cyclopentadienyl-type ligand are those of the general formula (I)
  • radicals X A in the general formula (I) are identical, preferably fluorine, chlorine, bromine, C 1 -C 7 -alkyl or arylalkyl, in particular chlorine, methyl or benzyl.
  • Particularly useful metallocenes of the formula (Ic) are those in which
  • the radicals R′ A are identical or different and are each hydrogen, C 1 -C 10 -alkyl or C 3 -C 10 -cycloalkyl, preferably methyl, ethyl, isopropyl or cyclohexyl, C 6 -C 20 -aryl, preferably phenyl, naphthyl or mesityl, C 7 -C 40 -arylalkyl, C 7 -C 40 -alkylaryl, preferably 4-tert-butylphenyl or 3,5-di-tert-butylphenyl, or C 8 -C 40 -arylalkenyl,
  • R 5A and R 13A are identical or different and are each hydrogen, C 1 -C 8 -alkyl, preferably methyl, ethyl, isopropyl, n-propyl, n-butyl, n-hexyl or tert-butyl,
  • rings S and T are identical or different and saturated, unsaturated or partially saturated.
  • the indenyl or tetrahydroindenyl ligands of the metallocenes of the formula (Ic′) are preferably substituted in the 2 position, the 2,4 positions, the 4,7 positions, the 2,4,7 positions, the 2,6 positions, the 2,4,6 positions, the 2,5,6 positions, the 2,4,5,6 positions or the 2,4,5,6,7 positions, in particular the 2,4 positions, with the following numbering applying to the site of substitution:
  • Particularly useful compounds of the general formula (Id) are those in which
  • organic transition metal compounds A) include metallocenes having at least one ligand derived from a cyclopentadienyl or heterocyclopentadienyl group having a fused-on heterocycle, with at least one carbon atom in the heterocycles being replaced by a heteroatom which is preferably selected from group 15 or 16 of the Periodic Table, in particular by nitrogen or sulfur.
  • metallocenes having at least one ligand derived from a cyclopentadienyl or heterocyclopentadienyl group having a fused-on heterocycle, with at least one carbon atom in the heterocycles being replaced by a heteroatom which is preferably selected from group 15 or 16 of the Periodic Table, in particular by nitrogen or sulfur.
  • transition metal is selected from among the elements Ti, Zr, Hf, Sc, V, Nb, Ta, Cr, Mo, W, Fe, Co, Ni, Pd, Pt and the elements of the rare earth metals. Preference is given to compounds having nickel, iron, cobalt or palladium as central metal.
  • E B is an element of group 15 of the Periodic Table of the Elements, preferably N or P, with particular preference being given to N.
  • the two or three atoms E B in a molecule can be identical or different.
  • transition metal complexes with ligands of the general formulae (IIa) to (IId) are, for example, complexes of the transition metals Fe, Co, Ni, Pd or Pt with ligands of the formula (IIa).
  • Particularly suitable compounds are those described in J. Am. Chem. Soc. 120, p. 4049 ff. (1998), J. Chem. Soc., Chem. Commun. 1998, 849.
  • Preferred complexes with ligands are 2,6-bis(imino)pyridyl complexes of the transition metals Fe, Co, Ni, Pd or Pt, in particular Fe.
  • Iminophenoxide complexes can also be used as organic transition metal compound.
  • the ligands of these complexes are prepared, for example, from substituted or unsubstituted salicylaldehydes and primary amines, in particular substituted or unsubstituted arylamines.
  • Transition metal complexes with pl ligands comprising one or more heteroatoms in the pl system for example the boratabenzene ligand, the pyrrolyl anion or the phospholyl anion, can also be used as organic transition metal compounds A).
  • transition metal compounds which are suitable for the purposes of the invention are substituted monocyclopentadienyl, monoindenyl, monofluorenyl or heterocyclopentadienyl complexes of chromium, molybdenum or tungsten in which at least one of the substituents of the cyclopentadienyl ring bears a rigid donor function which is not bound exclusively via sp 3 -hybridized carbon or silicon atoms.
  • the most direct link to the donor function in this case comprises at least one sp- or sp 2 -hybridized carbon atom, preferably from one to three sp 2 -hybridized carbon atoms.
  • the direct link preferably comprises an unsaturated double bond, an aromatic or together with the donor forms a partially unsaturated or aromatic heterocyclic system.
  • the cyclopentadienyl ring can also be a heterocyclopentadienyl ligand, i.e. at least one carbon atom can be replaced by a heteroatom of group 15 or 16. In this case, preference is given to a carbon atom in the C 5 ring being replaced by phosphorus.
  • the cyclopentadienyl ring is substituted by further alkyl groups which may also form a five- or six-membered ring such as tetrahydroindenyl, indenyl, benzindenyl or fluorenyl.
  • Possible donors are uncharged functional groups comprising an element of group 15 or 16 of the Periodic Table, e.g. amine, imine, carboxamide, carboxamide, carboxylic ester, ketone (oxo), ether, thioketone, phosphine, phosphite, phosphine oxide, sulfonyl, sulfonamide or unsubstituted, substituted or fused, partially unsaturated heterocyclic or heteroaromatic ring systems.
  • amine imine
  • carboxamide carboxamide
  • carboxylic ester ketone (oxo)
  • ketone (oxo) ketone
  • ether thioketone
  • phosphine phosphite
  • phosphine oxide sulfonyl
  • sulfonamide unsubstituted, substituted or fused, partially unsaturated heterocyclic or heteroaromatic ring systems.
  • the transition metal M C is chromium.
  • transition metal compounds which are suitable for the purposes of the invention are imidochromium compounds of the general formula (IV),
  • the catalyst system optionally comprises one or more activating compounds as cocatalysts.
  • Suitable cocatalysts are, for example, compounds such as an aluminoxane, a strong uncharged Lewis acid, an ionic compound having a Lewis-acid cation or an ionic compound having a Brönsted acid as cation. Preference is given to aluminoxanes.
  • a particularly useful aluminoxane is methylaluminoxane (MAO).
  • the amount of activating compounds to be used depends on the type of activator.
  • the molar ratio of metal complex to activating compound C) can be from 1:0.1 to 1:10000, preferably from 1:1 to 1:2000.
  • M 2D is an element of group 13 of the Periodic Table of the Elements, in particular B, Al or Ga, preferably B,
  • X 1D , X 2D and X 3D are each hydrogen, C 1 -C 10 -alkyl, C 6 -C 15 -aryl, alkylaryl, arylalkyl, haloalkyl or haloaryl each having from 1 to 10 carbon atoms in the alkyl radical and from 6 to 20 carbon atoms in the aryl radical or fluorine, chlorine, bromine or iodine, in particular haloaryls, preferably pentafluorophenyl.
  • Suitable ionic compounds having Lewis-acid cations include salt-like compounds of the cation of the general formula (XIII) [((M 3D ) a+ )Q 1 Q 2 . . . Q z ] d+ (XIII) where
  • Ionic compounds having Brönsted acids as cations preferably likewise have noncoordinating counterions.
  • Brönsted acid particular preference is given to protonated amine or aniline derivatives.
  • Preferred cations are N,N-dimethylanllinium, N,N-dimethylcylohexylammonium and N,N-dimethylbenzylammonium and also derivatives of the latter two. Further activating compounds are mentioned in WO 00/31090.
  • Suitable activating compounds C) also include boron-aluminum compounds such as di[bis(pentafluorophenyl)boroxy]methylalane. Examples of such boron-aluminum compounds are those disclosed in WO 99/06414.
  • Preferred mixtures comprise aluminoxanes, in particular methylaluminoxane, and an ionic compound, in particular one comprising the tetrakis(pentafluorophenyl)borate anion, and/or a strong uncharged Lewis acid, in particular tris(pentafluorophenyl)borane or a boroxine.
  • the organic transition metal compounds and, if appropriate, the activating compounds to be able to be used in polymerization processes in a gas-phase fluidized-bed reactor it is often advantageous, and preferred for the purposes of the invention, for them to be used in the form of a solid, i.e. for them to be applied to a solid support.
  • This method enables, for example, deposits in the reactor to be suppressed further or avoided and the polymer morphology to be controlled.
  • the unsupported catalyst system can be reacted with a support.
  • the order in which support, organic transition metal complex and the activating compound are combined is in principle immaterial.
  • the organic transition metal complex and the activating compound can be immobilized independently of one another, i.e. in succession, or simultaneously.
  • the support can firstly be brought into contact with the activating compound or compounds or the support can also firstly be brought into contact with the organic transition metal complex.
  • Preactivation of the organic transition metal complex with one or more activating compounds before mixing with the support is also possible.
  • the organic transition metal complex can also be prepared in the presence of the support.
  • the supports used preferably have a specific surface area in the range from 10 to 1000 m 2 /g, a pore volume in the range from 0.1 to 5 ml/g and a mean particle diameter of from 1 to 500 ⁇ m.
  • Particular preference is given to supports having a specific surface area in the range from 200 to 550 m 2 /g, a pore volume in the range from 0.5 to 3.0 ml/g and a mean particle diameter of from 10 to 150, in particular 30-1200 ⁇ m.
  • silica gel As inorganic support materials, preference is given to using silica gel, magnesium chloride, aluminum oxide, mesoporous materials, aluminosilicates and hydrotalcites. Particular preference is given to using silica gel, since particles whose size and structure may be suitable as supports for olefin polymerization can be produced from this material. Spray-dried silica gels comprising spherical agglomerates of smaller granular particles, i.e. primary particles, have been found to be particularly useful. The silica gels can be dried and/or calcined before use.
  • Suitable organic supports are, for example, polyethylene, polypropylene or polystyrene, which are preferably likewise freed of adhering moisture, solvent residues or other impurities by means of appropriate purification and drying operations before use. It is also possible to use functionalized, polar polymer supports, e.g. ones based on polystyrene, polyethylene, polypropylene or polytetrafluoroethylene, via whose functional groups, for example ammonium or hydroxy groups, at least one of the catalyst components can be immobilized.
  • functionalized, polar polymer supports e.g. ones based on polystyrene, polyethylene, polypropylene or polytetrafluoroethylene, via whose functional groups, for example ammonium or hydroxy groups, at least one of the catalyst components can be immobilized.
  • hybrid catalysts are mixtures of various catalysts, in particular two or more single-site catalysts. These can be present together on one support or can be used on separate supports.
  • the first and second catalysts can in principle be metered into the reactor in any way.
  • the metered addition is preferably carried out as described in EP-A-226 935 and DE-A-103 17 533.
  • a polymerization of ethylene with hexene as copolymer was carried out in a gas-phase fluidized-bed reactor having an output of 50 kg/h. Polymerizations were carried out using the following catalysts under the following conditions.
  • a hybrid catalyst based on a hafnocene and an iron-bisimine complex as described in DE 10 2005 035477 was used as catalyst.
  • a commercially available supported bis(indenyl)ZrCl2 metallocene catalyst was used as catalyst.
  • a Ziegler catalyst (Avant Z230M, Basell) was used as catalyst.
  • Catalyst changes involving the catalysts 1 to 4 were carried out using the following procedure:
  • the polymerization using the first catalyst was stopped by means of oxygen when the first catalyst was a chromium-based Phillips catalyst and by means of carbon dioxide in the case of all other catalysts.
  • a fresh fluidized bed charge was introduced and fluidized for a time of 12 hours by means of nitrogen with addition of a solution comprising 27 g of Costelan® AS 100 (commercial product of Costenoble GmbH, constituents: a polyethoxyalkylamine, a polyamino polyol and an alkylarylsulfonic acid), 27 g of Atmer® (manufactured by Uniqema, marketed by Ciba Spezi Rundenchemie GmbH, Germany), 4 l of 2-propanol and 4 l of hexane in an amount of 500 g/h at a temperature of 110° C. and a pressure of 2.0 MPa (20 bar).
  • Costelan® AS 100 commercial product of Costenoble GmbH, constituents: a polyethoxyalkylamine, a polyamino poly
  • the fluidized bed was subsequently discharged, the reactor was depressurized and opened.
  • the polymer particles remaining in the reactor were removed.
  • the reactor was closed and run moisture- and oxygen-free for a time of about 12-16 hours.
  • the new fluidized bed charge was subsequently introduced.
  • the reaction conditions prescribed for the respective catalyst were set and the polymerization was commenced as described above.
  • the results of the various catalyst changes are shown in the following table.
  • the total time for the catalyst change was about 33-37 hours.
  • the products obtained using the second catalyst were processed on a film blowing machine to produce films.
  • Catalyst changes involving the catalysts 1 to 4 were carried out using the following procedure:
  • the polymerization using the first catalyst was stopped by means of oxygen when the first catalyst was a chromium-based Phillips catalyst and by means of carbon dioxide in the case of all other catalysts.
  • a fresh fluidized bed charge was introduced and fluidized for a time of 6 hours by means of nitrogen with addition of a solution comprising 27 g of Costelan® AS 100 (commercial product of Costenoble GmbH), 27 g of Atmer® (manufactured by Uniqema, marketed by Ciba Spezialitätenchemie GmbH, Germany), 4 l of 2-propanol and 4 l of hexane in an amount of 300 g/h at a temperature of 110° C. (1° C. below the sintering temperature) and a pressure of 2.0 MPa (20 bar).
  • the fluidized bed was subsequently discharged, the reactor was depressurized and opened.
  • the polymer particles remaining in the reactor were removed.
  • the reactor was closed and run moisture- and oxygen-free for a time of about 8 hours.
  • the new fluidized bed charge was subsequently introduced.
  • the reaction conditions prescribed for the respective catalyst were set and the polymerization was commenced as described above.
  • the results of the various catalyst changes are shown in the following table.
  • the total time for the catalyst change was about 16 hours.
  • the products obtained using the second catalyst were processed on a film blowing machine to produce films.
  • the polymerization using the first catalyst was stopped by means of oxygen as volatile deactivating agent when the first catalyst was a chromium-based Phillips catalyst and by means of carbon dioxide in the case of all other catalysts.
  • the fluidized bed was subsequently discharged, the reactor was depressurized and opened.
  • the polymer particles remaining in the reactor were removed.
  • the reactor was cleaned using water as further volatile deactivating agent for a time of about 8 hours. All ports were subsequently opened and dried for a time of about 12 hours.
  • the reactor was closed and run moisture- and oxygen-free for a time of about 48 hours.
  • the new fluidized bed charge was subsequently introduced.
  • the total time for the catalyst change was about 71 hours.
  • the products obtained using the second catalyst were processed on a film blowing machine to produce films.
  • the polymerization using the first catalyst was stopped by means of oxygen as volatile deactivating agent when the first catalyst was a chromium-based Phillips catalyst and by means of carbon dioxide in the case of all other catalysts.
  • the fluidized bed was subsequently discharged, the reactor was depressurized and opened. The polymer particles remaining in the reactor were removed. The reactor was closed and run moisture- and oxygen-free for a time of about 12-16 hours.
  • the new fluidized bed charge was subsequently introduced.
  • the total time for the catalyst change ranged from 40 hours to a number of days.
  • the products obtained using the second catalyst were processed on a film blowing machine to produce films.
  • a catalyst change from catalyst 1 to catalyst 2 was carried out using the following procedure:
  • the polymerization using the first catalyst was stopped by means of oxygen as volatile deactivating agent.
  • the fluidized bed was subsequently discharged, the reactor was depressurized and opened.
  • the polymer particles remaining in the reactor were removed.
  • the reactor was cleaned using isopropanol as volatile deactivating agent for a time of about 8 hours.
  • the reactor was closed and run moisture- and oxygen-free for a time of about 12-16 hours.
  • the new fluidized bed charge was subsequently introduced.
  • the reaction conditions prescribed for the respective catalyst were set and the polymerization was commenced.
  • the total time for the catalyst change was 70 hours. Slightly increased electrostatic charging in the dry reactor was observed. The product had an increased proportion of fines having particle sizes of ⁇ 125 ⁇ m.
  • the products obtained using the second catalyst were processed on a film blowing machine to produce films.
  • a catalyst change from catalyst 1 to catalyst 2 was carried out using the following procedure:
  • the polymerization using the first catalyst was stopped by means of oxygen as volatile deactivating agent.
  • the fluidized bed was subsequently discharged, the reactor was depressurized and opened.
  • the polymer particles remaining in the reactor were removed.
  • a fresh fluidized bed charge was introduced and was fluidized for a time of 12 hours by means of nitrogen with addition of 27 g of Costelan® AS 100 (commercial product of Costenoble GmbH), 27 g of Atmer® (manufactured by Uniqema, marketed by Ciba Spezialitätenchemie GmbH, Germany) in 4 l of hexane in an amount of 500 g/h at a temperature of 110° C. and a pressure of 2.0 MPa (20 bar).
  • the new fluidized bed charge was subsequently introduced.
  • the reaction conditions prescribed for catalyst 2 were set and the polymerization was commenced as described above.
  • the total time for the catalyst change was 35 hours. Deposits were formed in the reactor. The course of the polymerization was subject to large fluctuations. The reactor had to be shutdown after 10 hours because of a blocked discharge line.

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WO2010009860A1 (fr) 2008-07-23 2010-01-28 Basell Polyolefine Gmbh Procédé de transition entre des systèmes catalytiques de polymérisation d’oléfines incompatibles
SG171988A1 (en) 2008-12-23 2011-07-28 Basell Polyolefine Gmbh Method for transitioning between incompatible olefin polymerization catalyst systems
US8148470B1 (en) 2010-11-19 2012-04-03 Exxonmobil Chemical Patents Inc. Processes for making multimodal molecular weight distribution polyolefins
CN103052655B (zh) * 2010-11-19 2015-05-13 埃克森美孚化学专利公司 多峰态分子量分布聚烯烃的制备方法
US9914794B2 (en) * 2014-05-27 2018-03-13 Sabic Global Technologies B.V. Process for transitioning between incompatible catalysts
KR20170109548A (ko) 2014-12-22 2017-09-29 사빅 글로벌 테크놀러지스 비.브이. 비융화성 촉매 간의 전환 방법
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CN101316870B (zh) 2011-01-12
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CN101316870A (zh) 2008-12-03
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EP1954725A1 (fr) 2008-08-13

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